TWI352614B - Process and plant for the simultaneous production - Google Patents

Process and plant for the simultaneous production Download PDF

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Publication number
TWI352614B
TWI352614B TW093115702A TW93115702A TWI352614B TW I352614 B TWI352614 B TW I352614B TW 093115702 A TW093115702 A TW 093115702A TW 93115702 A TW93115702 A TW 93115702A TW I352614 B TWI352614 B TW I352614B
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TW
Taiwan
Prior art keywords
natural gas
stream
pretreated
liquefiable
purified
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Application number
TW093115702A
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English (en)
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TW200503815A (en
Inventor
Henri Paradowski
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Technip France
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Publication of TW200503815A publication Critical patent/TW200503815A/zh
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Publication of TWI352614B publication Critical patent/TWI352614B/zh

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0057—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream after expansion of the liquid refrigerant stream with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • F25J1/0215—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
    • F25J1/0216—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle using a C3 pre-cooling cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
    • F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

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  • Engineering & Computer Science (AREA)
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1352614 玫、發明說明 【發明所屬之技術領域】 本發明係關於一種從一含有氮、甲烷、c2至c5烴類 以及C6 +重質烴類之天然氣進料（1〇1)中同時製造可液 化天然氣（161)及天然氣液體（NGL )餾份（15 )之方 法及設備。 【先前技術】 已知之天然氣液化設備連續地包括製造可液化氣體之 單元，實質地進行液化之單元，以及可除去LNG中之氮 氣的單元。該用於製造可液化氣體之單元必然包括除去 C6 +重質烴類（其會於液化期間結晶）之構件。 爲了同時製造可液化天然氣及NGLs，可行的是使用 如前述形態之方法，舉例之如申請案FR-A-2 8 1 7 766案 號所揭示之方法。 此一方法具有熱力效率，最適於在室溫下製造天然氣 及NGL之提取。 結果，若所製得之天然氣必須液化，則此一方法並無 法令人完全滿意。此乃因爲欲使製得之天然氣液化所需的 能量支出相當高。 本發明之主要目標係補救此一缺點，也就是說係提供 一種供用於同時製造LNG及NGL餾份之方法，其將比現 存之方法更具經濟效益且更有彈性。 1*352614 【發明內容】 本發明係關於一種從一含有氮、甲烷、c2至c5烴類 以及c6+重質烴類之天然氣進料中同時製造可液化天然氣 及天然氣液體（NGL )餾份的方法，該方法包括下列之步 驟： (a) 預處理該天然氣進料以便獲得一預處理之天然 氣： (b) 將源自步驟（a)之預處理天然氣冷卻至接近其 露點之溫度： (c) 使源自步驟（b)之冷卻的預處理天然氣膨脹， 並將此膨脹之天然氣導入一含有至少一個主蒸餾塔（49) 之NGL回收單元，如此一方面可產生做爲塔頂產物之純 化天然氣，且另一方面可產生該NGL餾份；及 (d) 從源自步驟（c)之已純化天然氣中生成該可液 化天然氣。 本發明之方法係施加在用於從地底下提取之天然氣中 製造液化天然氣（稱之爲"LNG〃 ）做爲主產物並以天然 氣液體（稱爲"NGL〃 ）餾份爲副產物的設備上。 在本發明中，NGL可理解地是表示從天然氣中提取 之C2 +至C3 +烴類。經由實例說明，這些NGLs可包括乙 烷、丙烷、丁烷及C5 +烴類。 在提取NGLs後所產生之LNG擁有比不提取NGLs所 產生之LNG還低的熱値。
S -6- 1352614 【實施方式】 基於此一目的，本發明之目標係一具有前述形態之方 法，且其特徵爲步驟（a)包括下列之子步驟： (al)將天然氣進料冷卻至一接近其露點之溫度； (a2)將源自步驟（al)之該冷卻的天然氣進料導入 一輔助蒸餾塔內，以產生做爲頂部產物之該預處理之天然 氣，且此預處理天然氣實質上不再含有任何C6 +烴類，再 者此第一輔助蒸餾塔可產生一基本上帶有C6 +重質烴類之 餾份。 依據本發明，該方法可各別地或依任何可能之組合方 式涵蓋一或多個下列之特徵： -步驟（d)可包括下列之子步驟： (dl)在至少第一壓縮機內並於一液化壓力下使從該 主塔頂部提取之已純化天然氣壓縮；及 (d2)源自步驟（dl)之經壓縮已純化天然氣將在第 一熱交換器中藉由與該從主塔頂部所提取之已純化天然氣 進行熱交換而冷卻，以便產生可液化天然氣； —步驟（b)可包括下列之子步驟： (bl)源自步驟（a)之預處理天然氣將在第二熱交 換器中藉由與該從第二主塔所提取之已純化天然氣進行熱 交換而冷卻； -步驟（c)可包括下列之子步驟： (cl)將源自步驟（b)之冷卻的預處理天然氣導入 —分離滾筒，以便獲得液體股流及氣體股流： 1-352.614 (c2)在一連結至第一壓縮機之渦輪機內使源自步驟 (c 1 )之氣體股流膨脹； (c3 )在一中間水平N3處下將源自步驟（c2 )之股 流導入主塔中；以及 (c4)使源自步驟（cl)之液體股流膨脹，並在一低 於水平N3之水平N2處將此膨脹之液體股流導入主塔中
I 一在步驟（dl)中，該經由該第一壓縮機輸出之已壓 縮純化天然氣可在供應有外來能源之第二壓縮機中壓縮， 以便達成該液化壓力； -主蒸餾塔之壓力是大於35巴； -可液化天然氣將進一步包含一部份直接來自步驟（ a)之預處理天然氣； —此方法包括一啓動階段（start-up phase)，其中可 液化天然氣主要地或完全地係由直接來自步驟（a)之預 處理天然氣所組成，且該可液化天然氣相當富含C2至C5 烴類，同時此方法還包括一隨後之製造階段，其中，在可 液化天然氣中部份直接來自步驟（a)之預處理天然氣將 根據該可液化天然氣所需之C2至C5烴類含量來調整；以 及 -使一藉由輔助塔產生之液體膨脹，再將之導入主塔 〇 同時’本發明之目標也係一種用於從含有氮、甲烷' C2至C5烴類以及c6 +重質烴類之天然氣進料中同時製造
S -8 - 1352614 可液化天然氣及天然氣液體（NGL )餾份的設備，該形態 包括： (a) 可用於預處理該天然氣進料以便獲得一預處理 之天然氣的單元； (b) 可用於將該預處理天然氣冷卻至接近其露點之 溫度的構件； (e )回收NGLs之單元，其包括可使該冷卻之預處 理天然氣膨脹的構件及至少一個主蒸餾塔，如此一方面可 產生做爲塔頂產物之純化天然氣，且另一方面可產生該 NGL餾份；以及 (d)將該源自步驟（c)之已純化天然氣送入一可液 化天然氣管線內之構件； 此設備之特徵爲，該預處理單元可包括； (a 1 )將天然氣進料冷卻至一接近其露點之溫度的構 件；及 (a2)用於蒸餾該冷卻之天然氣進料的輔助蒸餾塔， 以產生做爲頂部產物之該預處理之天然氣，且此預處理天 然氣實質上不再含有任何C6 +烴類，再者此輔助蒸餾塔可 產生一基本上帶有C6 +重質烴類之餾份。 依據本發明，該設備可各別地或依任何可能之組合方 式涵蓋一或多個下列之特徵： -該生成可液化天然氣之構件可包括： (dl)用於在一液化壓力下使從該主塔頂部提取之已 純化天然氣壓縮的構件，彼包括至少第一壓縮機；及 -9- 1-352.614 (d2)將來自該壓縮構件之經壓縮已純化天然氣與該 從主塔頂部所提取之已純化天然氣引入熱交換關係的第一 熱交換器中，該經壓縮已純化天然氣在此第一熱交換器中 冷卻以便產生可液化天然氣； -該用於冷卻預處理天然氣之構件包括了可將此氣體 與該從主塔所提取之已純化天然氣引入熱交換關係的第二 熱交換器； —該回收NGLs之單元可包括： (cl)用於分離該冷卻之預處理天然氣的分離滾筒， 此分離滾筒可產生液體股流及氣體股流； ()用於使該氣體股流膨脹之第一膨脹渦輪機，該 渦輪機係連結至該第一壓縮機； (c3 )用於在一中間水平N3處將該膨脹之氣體股流 導入主塔的構件；以及 (c4)使該液體股流膨脹之構件及在一低於N3之水 平N2處將此膨脹之液體股流導入主塔的構件； 一用於壓縮該從主塔頂部所提取之已純化天然氣的構 件，其進一步包括藉由外來能源驅動之第二壓縮機並乃意 圖使該經壓縮之已純化天然氣的壓力增高至可液化壓力； 及 -用於生成已純化天然氣之構件’其包括將直接來自 預處理單元之預處理天然氣的可調整部份選擇性地導入— 可液化天然氣管線之構件。 執行本發明之實施例將與隨附之單一圖示結合而說明
S -10- 1352614 如下，該圖係顯示一可解說如本發明之設備如何操作的槪 要圖。 圖中所顯示之設備係關於從一具有乾燥、脫碳及脫硫 之天然氣進料來源11中同時製造做爲主產物之LNG 13 及副產物之NGL餾份15。此設備包括用於除去C6 +重質 烴類之單元17、用於回收NGLs之單元19及液化單元21 〇 如本文以下所述，一液體股流及傳送此股流之管線將 以相同之參考符號表示，而壓力則無疑地係爲絕對壓力》 用於除去重質烴類之單元17係連續地包括來源11下 游之第一、第二及第三冷卻器25、27、29，以及裝設有 頂部冷凝器的第一蒸餾塔或輔助蒸餾塔31。此冷凝器包 括，在該第一蒸餾塔31與第一分離滾筒33之間，於其中 —側的第四冷卻器3 5及在另一側的回流泵3 7。 NGL回收單元19包括第一、第二及第三熱交換器41 、43、45，第二分離滾筒47，第二蒸餾塔或主蒸餾塔49 ，連結至第一壓縮機53之第一渦輪機51、藉由外來能源 56驅動之第二壓縮機55，第五冷卻器57及NGL提取泵 59 ° 天然氣液化單元21包括第四、第五熱交換器65、67 ，彼等可藉由一冷凍循環69來冷卻。 此循環69包括帶有三階段73A、73B、73C之壓縮機 (且該等壓縮機提供有第一及第二中間冷卻器75A及75B 及後冷卻器75C)，串聯之四個冷卻器77A至77D，第三 -11 - Γ352614 分離滾筒79，以及第一及第二液壓渦輪機81及83。 執行如本發明之方法的實施例將說明如下。 具有乾燥、脫碳及脫硫之天然氣進料的股流1〇1其最 初莫耳組成份包含3.90%氮、87.03%甲烷、5.50%乙烷 ' 2.00% 丙烷、0·34% 異 丁烷、0.54% 正一 丁烷、0.18% 異戊烷、0.15%正一戊烷、0.31% C6烴類' 0.03% C7 烴類及0.02% C8烴類。 此氣體101將連續地在第一、第二及第三冷卻器25 、27、29中冷卻以便形成冷卻之天然氣進料103。然後將 此氣體103導入蒸餾塔31。此塔31可產生帶有C6 +重質 烴類之餾份1 05以做爲底部產物。此餾份1 05將在膨脹閥 1 06內膨脹以產生一帶有重質烴類之膨脹股流1 07，其將 在低水平N1處導入第二蒸餾塔49。 此外，該第一蒸餾塔31還產生一帶有預處理氣體之 股流以做爲頂部產物。在第四冷卻器3 5中冷卻此股流 109並使之部份冷凝，然後導入第一分離滾筒33，在其內 將分離成一組成預處理天然氣111之氣相及一組成回流液 體1 1 2之液相，該液體將藉由回流泵3 7以回流方式返回 純化塔中。 該預處理天然氣111之莫耳組成份包含3.9783%氮、 88.203 6 % 甲烷、5.3 622 % 乙烷、1.75 5 0 % 丙烷、0.2488% 異 丁烷、0.3 465 % 正-丁烷、0.0616% 異戊烷、0.03 84% 正一戊烷及0.005 7 % C6烴類。 此C6烴類幾乎已完全從此股流111中除去^
S -12- 1352614 然後，將該預處理天然氣股流111分開成 NGL回收單元19之股流113及一可送至氣體液 之股流1 1 5。在兩股流之間的分開過程可經由控 別的控制閥1 1 4及1 1 6而有所選擇。 導入回收單元19之股流113將在第二熱交g 冷卻’以便獲得具有冷卻之預處理天然氣的兩相 。將此股流117導入第二分離滾筒47，其將產 流1 1 9及液體股流1 2 1。在膨脹閥1 23內使液體 膨脹，然後在高於水平N1之水平N2處將之導？ 〇 蒸氣股流119將分離成主要餾份125及次要 〇 在渦輪機5 1中使主要餾份1 2 5膨脹以便得 之主要餾份129，並在高於水平N2之水平N3處 塔49中。 次要餾份I27將在熱交換器45中冷卻，並 131內膨脹，然後在高水平N4處導入塔49中。 是比水平N3還高。 塔49也可裝設一中間再沸器141。一再沸器 可在低於N2但高於N1之水平Nla處從此塔中 此股流可在第二熱交換器4 3中加溫，再於水平 平N1之間的水平Nib處導入第二塔49中。 藉由泵59從蒸餾塔49之底部提取出NGL食 此外，底部再沸器145是安裝在塔49上以便調璧 一可送入 化單元21 制兩個各 I器43中 股流1 1 7 生蒸氣股 股流1 2 1 、塔49中 餾份127 到一膨脹 將之導入 於膨脹閥 水平N4 股流143 提取出。 N 1 a與水 留份1 5。 套NGL中 -13- Γ352614 C !烴類相對於C2烴類的莫耳比。此比率較佳地是小於 0.02。 因此，此NGL餾份15含有0.3688%甲烷、36.8810 % 乙院、33.8344 丙院 ' 6.1957% 異丁垸、9.9267% 正一 丁烷、3.3354% 異戊烷、2.7808% 正一戊烷、5.749 8% C6 烴類、0.5 5 64 % C7 烴類及 0.3710% C8 烴類。 乙烷、丙烷及C4+烴類提取中之各別量是36.15%、 91.21%及99.3%。因此，經由如本發明之方法回收的乙 烷量係大於30%。回收的丙烷量大於80% ’較佳地是大 於90%。回收的C4+烴類量是大於90%，較佳地是大於 95%。 純化之天然氣股流1 5 1是以頂部產物方式從塔49中 提取而得。此股流151將在熱交換器45、熱交換器43及 接續之熱交換器4 1中連續加溫。應指出的是，在操作 NGL回收單元19時是不需要外來冷源。 然後，將來自熱交換器4 1之已加溫氣體股流1 5 3連 續地於壓縮機51及第二壓縮機55中壓縮以便在液化壓力 下產生一氣體股流1 5 5。 在第五冷卻器5 7及第一熱交換器4 1中冷卻以獲得一 冷卻之純化氣體股流1 5 7。將此股流1 5 7與剛從單元1 7 ( 用於除去C6+重質烴類）中提取且欲送入氣體液化單元 之股流1 15混合。股流157和股流1 15股流具有幾乎相同 之溫度及壓力，並可一起形成帶有天然氣之股流161。 此帶有天然氣之股流1 61的莫耳組成份包含4.1 22 1 % β -14- 1352614 氮、91.9686% 甲烷、3.7118% 乙烷、0.1858% 丙烷、 0.0063% 異 丁院、0.0051% 正—丁院及 0.0003% C5"1"煙類 〇 然後，將此帶有天然氣之股流161連續地在第四及第 五熱交換器65、67中冷卻，以便產生LNG股流13。接 著，在單元165中使此LNG股流13進行氮氣脫除步驟。 在第四及第五熱交換器65、67中進行冷動將可提供 —冷凍混合物股流201。此股流201將部份地在第四冷卻 器冷卻器77D中液化，並導入分離滾筒79內，然後分離 成蒸氣相2 0 3及液相2 0 5。 此股流2 0 1及蒸氣相和液相2 0 3與2 0 5之莫耳組成份 乃如下列： 股流20 1 (%) 股流203(%) 股流 ‘2 05 (%) N2 4.0 10.18 1.94 C 1 42.4 67.90 3 3.90 C2 42.6 20.18 50.07 C3 11.0 1.74 14.09 蒸氣相203可於熱交換器65中液化以得到一液體股 流，接著在第五熱交換器67中再使之過冷，即可獲得過 冷之液體股流207。 將此過冷之液體股流2 0 7於第一液壓渦輪機8 1中膨 脹，然後再於膨脹閥20 8內膨脹，即可獲得第一冷凍股流 209。在熱交換器67中使股流209蒸發並可同時讓氣體 -15- Γ352614 1 6 1液化。 在交換器65中使液相205過冷以得到一過冷股流， 依序地再於第二液壓渦輪機83及膨脹閥210中膨脹，即 可得到第二冷凍股流2 1 1。股流209及2 1 1將混合一起以 形成一組合股流213，其將在交換器65蒸發。此蒸發作 用可使股流161冷卻，並使冷凍混合物股流201中之蒸氣 相2〇3冷凝。然後，將此組合股流213於壓縮機77中壓 縮，以便製得一壓縮之混合物股流215，其特徵乃示於下 表中8 壓縮機 73 A 73B 73C 抽吸溫度（°C ) -37.44 34 34 排出溫‘度（°c ) 67.25 68.70 68.15 抽吸壓力（巴） 3.65 18.30 29.70 排出壓力（巴） 18.70 3 0.00 47.6 1 多變性效率（％) 82 82 82 功率 74 109 24396 2 1882 然後’將此壓縮之混合物股流215連續地於四個串聯 之冷卻器8 1中冷卻，以便形成股流20 1。 一方面，用於冷卻天然氣進料之第一 '第二、第三及 第四冷卻器25、27、29、35’及另一方面用於冷卻混合 物股流201之四個冷卻器77A至77D都是使用相同的丙 垸冷凍循環（未顯現）。此循環包括四個下列之蒸發階段
S -16- 1352614 :6.7°C/7.92 巴；0°C/4.76 巴；一20°C/ —36°C/1_30 巴。 如圖所示之設備的操作溫度、壓力及流 由下表之實施例而定。 2.44 巴； 速之模擬乃經 -17- 1352614 θ 溫度 壓力 流速 股流 (%) (巴） (公斤/小時） 13 -1 48 58.9 809567 15 78 43.2 123436 10 1 23 62.0 933003 103 -1 8 6 1.1 933003 105 -1 8 6 1.1 498 88 107 -23 39.8 498 8 8 111 -34 60.8 883115 113 -34 60.8 883115 115 _ 0 117 -47 60. 1 883115 123 -59 39.8 3 6469 129 -66 39.8 675718 13 1 -86 39.8 178092 143 -48 39.6 124894 15 1 -76 39.5 809567 153 32 38.8 809567 155 74 61.5 809567 157 -34.6 60.1 809567 16 1 -34.6 60.1 809567 20 1 -34 46.1 1510738 207 -1 48 44.9 303816 209 -1 54 4.2 303816 2 11 -1 3 0 4.1 1206922 2 13 -1 28 4.1 1510738 2 15 34 47.6 1510738 -18- 1352614 如此實施例所解說，蒸餾塔3 1之壓力較佳地係在45 至65巴之間。第二塔之壓力較佳地係大於35巴。 依此，使每一塔之操作達到最佳化就變得可行，如此 一方面有利於塔3 1之C6 +烴類的提取，另一方面則利於 塔49之乙烷及丙烷的提取。 此外，純化之氣體股流157及欲送入氣體液化單元之 股流115是在高於55巴之壓力下產生。 因此，本方法可使達成如下所述之能源節省變得可行 ，其是將先前技藝（沒有輔助塔31)之耗損功率與如本 發明之設備的耗損功率做比較。 更精確地說，在先前技藝中天然氣進料股流101是直 接送入NGL提取單元19並使用丙烷循環之冷卻器25、 27、29及35 (這些冷卻器也充當來預先冷卻在液化壓力 下之氣體股流丨55) ’不像本發明之設備使用了熱交換器 41來執行此一預先冷卻。 先前技藝 如本發明之方法 混合冷凍之壓縮機73(kW) 119460 120387 丙烷冷凍之壓縮機（未顯示） (kW) 69700 72 174 處理氣體之壓縮機55(kW) 20650 14964 共計（kW) 209810 207525 所以’在與先前技藝之設備比較時，如本發明之設備 -19- 1352.614 可同時製造LNG 13及NGL餾份15，並能節省2285 kW 〇 而且，當啓動本發明之設備時，所有來自該用於除去 重質烴類之單元17的預處理天然氣股流111經由進料股 流Π5而直接被送入液化單元21中。所以，製得之LNG 具有相當高的熱値。接著，NGL回收單元19漸進地啓動 ，且不會影響液化單元21之生產力。然後，藉由送進 NGL回收單元之進料股流113及送進氣體液化單元之股 流1 1 5的相對流速來調整所得之LNG的熱値。 同樣地，如NGL回收單元1 9所發生般，所有來自重 質烴類排除單元17之預處理天然氣股流111將經由進料 股流1 1 5而直接送入液化單元2 1中。 至於變異方面，NGL回收單元可包括安裝在第二蒸 餾塔下游之第三蒸餾塔，其是在比第二蒸餾塔還低或還高 的壓力下操作。此第三蒸餾塔可用來濃縮具有特定組份（ 如丙烷）之NGLs。此一單元之實施例係揭示於歐洲專利 ΕΡ-Α-0 5 3 5 752 案號中。 由於本發明之揭示使得擁有一以更經濟且更彈性之方 式同時製造LNG及NGLs並且在C2至C5烴類提取時具有 高量的設備變得可行。令人驚喜地，藉由在NGL回收單 元之上游插入一輔助性蒸餾塔，並藉由將此塔之頂部產物 餾份導入此一單元中便能顯著地減低能量耗損。 此一設備之生產力是因著能將至少一部份此頂部產物 餾份直接導入液化單元而增加，特別是在設備啓動階段之
S -20- 1352614 期間或假若NGL回收單元故障時。 而且，此一設備能製造一具有可調整之熱値的NGLs 【圖式簡單說明】 圖1 / 1係顯示一可解說如本發明之設備及如何操作 的槪要圖。 【主 要元 件 符 Orfe Wi 說 明 ] 11 來 源 13 可 液 化 天 然 氣 股 流 15 天 然 氣 液 體 餾 份 17 用 於 除 去 重 質 烴 類 之 單 元 19 回 收 NGLs 之 單 元 2 1 液 化 單 元 25 第 —* 冷 卻 器 27 第 二 冷 卻 器 29 第 二 冷 卻 器 3 1 第 -* 蒸 餾 塔 或 輔 助 蒸 餾 塔 32 頂 部 冷 凝 器 33 第 一 分 離 滾 筒 35 第 四 冷 卻 器 37 回 流 泵 4 1 第 一 熱 交 換 器 -21 - 1352614 43 第 二 熱 交 換 器 45 第 三 熱 交 換 器 47 第 二 分 離 滾 筒 49 第 二 蒸 餾 塔 或 主蒸餾塔 5 1 第 — 渦 輪 機 53 第 一 壓 縮 機 5 5 第 二 壓 縮 機 56 外 來 能 源 57 第 五 冷 卻 器 59 NGL 提 取 泵 65 第 四 熱 交 換 器 67 第 五 熱 交 換 器 69 致 冷 循 環 73 壓 縮 機 73 A 第 —- 階 段 73B 第 二 階 段 73C 第 二 階 段 75 A 第 一 中 間 冷 卻 器 75B 第 二 中 間 冷 卻 器 75C 後 冷 卻 器 77A 冷 卻 器 77B 冷 卻 器 11C 冷 卻 器 77D 冷 卻 器 s -22- 第三分離滚筒 第一液壓渦輪機 第二液壓渦輪機 天然氣進料之股流 冷卻之天然氣進料 做爲底部產物之餾份 膨脹閥 已膨脹股流 做爲頂部產物之股流 預處理天然氣 回流液體 股流 控制閥 股流 控制閥 兩相股流 蒸氣股流 液體股流 膨脹閥 主要餾份 次要餾份 膨脹之主要餾份 膨脹閥 中間再沸器 -23- 1352614 143 再沸器股流 15 1 純化之天然氣股流 153 加溫之氣體股流 155 氣體股流 157 冷卻之純化氣體股流 16 1 股流 16 5 單元 201 冷凍混合物股流 203 蒸氣相 205 液相 207 過冷之液體股流 208 膨脹閥 209 第一冷凍股流 210 膨脹閥 211 第二冷凍股流 213 組合股流 2 15 壓縮之混合物股流 N1 低水平
Nla 低於N2但高於N1之水平
Nib 於水平N 1 a與水平N 1之間的水平 N2 高於水平N1之水平 N3 高於水平N2之水平 N 4 高水平 NG 天然氣
S -24- 1352614 NGL 天然氣液體 LNG 可液化天然氣

Claims (1)

1352614 拾、申請專利範圍 1. 一種從含有氮、甲烷' 〇2至c5烴類以及c6 +重質 烴類之天然氣進料（101)同時製造可液化天然氣（161) 及天然氣液體（NGL )餾份（15 )的方法； 該方法包括下列之步驟： (a) 預處理該天然氣進料（1〇1)以便獲得預處理之 天然氣（1 1 1 ); (b) 將源自步驟（a)之預處理天然氣（111)冷卻 至接近其露點之溫度； (c) 使源自步驟（b)之冷卻的預處理天然氣（117 )膨脹，並將此膨脹之天然氣（121、127、129)導入含 有至少一個主蒸餾塔（49)之NGL回收單元（19)，如 此一方面產生做爲塔頂產物之純化天然氣（1 5 1 )，且另 一方面產生該NGL餾份（15 );及 (d) 從源自步驟（C)之純化天然氣（Ml)中生成 該可液化天然氣（1 6 1 ); 其特徵爲，步驟（a)包括下列子步驟： (al)將天然氣進料（101)冷卻至接近其露點之溫 度； (a2)將源自步驟（al)之該冷卻的天然氣進料（ 103)導入一裝設有產生回流之頂部冷凝器（32)的輔助 蒸餾塔（31)內，此輔助蒸餾塔（31)係在45至65巴之 壓力下操作，並產生做爲頂部產物之該預處理天然氣（ 111)，此預處理天然氣（111)實際上不再含有任何C6 + S -26- 1352614 烴類，此輔助蒸餾塔（31)還產生基本上C6+重質烴類 之餾份（1〇5 ); 步驟（c)包括下列子步驟： (cl)將源自步驟（b)之冷卻的預處理天然氣（117 )導入分離滾筒（47 )，以便獲得液體股流（1 2 1 )及氣 體股流（1 2 5 ); (c2)在連結至第一壓縮機（53)之渦輪機（51)內 使源自步驟（cl)之氣體股流（125)膨脹； (c3 )將源自步驟（c2 )之股流（129 )從該主塔（ 49)的中間水平N3處導入該主塔（49)中；以及 (c4 )使源自步驟（cl )之液體股流（121 )膨脹， 並將此膨脹之液體股流（1 2 1 )從該主塔（49 )之低於水 平N3的水平N2處導入該主塔（49)中； 而且，該可液化天然氣（161)還包含該直接來自步 驟（a)之預處理天然氣（111)的一部份（115)。 2. 如申請專利範圍第1項之方法，其中，步驟（d ) 包括下列子步驟： (dl)在至少該第一壓縮機（53)內於液化壓力下將 從該主塔（49)頂部提取之純化天然氣（151)壓縮；及 (d2 )將源自步驟（d 1 )之經壓縮的純化天然氣（ 155)在一第一熱交換器（41)中藉由與從該主塔（49) 頂部所提取之該純化天然氣（1 5 1 )進行熱交換而冷卻’ 以便產生該可液化天然氣（1 6 1 )。 3. 如申請專利範圍第2項之方法，其中，步驟（b ) -27- 1352614 包括以下子步驟： (bl)將源自步驟（a)之預處理天然氣（113)在一 第二熱交換器（43)中藉由與從該主塔（49)所提取之純 化天然氣（151)進行熱交換而冷卻。 4. 如申請專利範圍第2或3項之方法，其中，在步 驟（dl)中，該經由該第一壓縮機（53)輸出之已壓縮純 化天然氣（153 )係在供應有外來能源（56 )之第二壓縮 機（5 5 )中壓縮，以便達到該液化壓力。 5. 如申請專利範圍第1至3項中任一項之方法，其 中該主蒸餾塔（49)之壓力係大於35巴。 6_如申請專利範圍第1至3項中任一項之方法，該 方法包括一啓動階段，其中該可液化天然氣（161)主要 地或完全地係由直接來自步驟（a)之預處理天然氣（111 )所組成，且該可液化天然氣（161 )相對富含C2至C5 烴類，該方法還包括一隨後之製造階段，其中，該可液化 天然氣（161)中直接來自步驟（a)之預處理天然氣（ 1 1 1 )的部份（1 1 5 )係根據該可液化天然氣（1 6 1 )中所 需之C2至C5烴類含量來調整。 7. 如申請專利範圍第1至3項中任一項之方法，其 中將經由該輔助塔（31)產生之液體（105)膨脹並導入 該主塔（49 )。 8. 如申請專利範圍第1至3項中任一項之方法，其 中，該輔助蒸餾塔（31)係被設計以提取存在於該天然氣 進料（101)內的約98莫耳％之c6+烴類。 S -28- 1352614 9·如申請專利範圍第1至3項中任一項之方法，其 中，該預處理天然氣（111)中之C6+烴類的.莫耳含量係 約等於57ppm。 10.—種用於從含有氮、甲烷、至C5烴類以及 重質烴類之天然氣進料（ι〇1)中同時製造可液化天然 氣（16丨）及天然氣液體（NGL)餾份（15)的設備，該 設備包括： (a) 用於預處理該天然氣進料（11)以便獲得預處 理之天然氣（111)的單元（17); (b) 用於將該預處理天然氣（1Π)冷卻至接近其露 點之溫度的構件（43 ): (c) 用於回收NGLs之單元（19)，其包括用於使 該冷卻之預處理天然氣（117)膨脹的構件（51、123、 131)，其並包括至少一個主蒸餾塔（49)，此主蒸餾塔 (4 9 )—方面產生做爲塔頂產物之純化天然氣（1 5 1 )， 且另一方面產生該NGL餾份（15):及 (d) 用於從該源自步驟（c)之純化天然氣（151) 中生成該可液化天然氣的構件（53、55、41); 其特徵爲，該預處理單元（17)包括； (al)用於將該天然氣進料（101)冷卻至接近其露 點之溫度的構件（25、27、29);及 (a2)用於蒸餾該冷卻之天然氣進料（103)的輔助 蒸餾塔（31)，此輔助塔裝設有一產生回流之頂部空冷凝 器（32)，該輔助蒸餾塔（31)係在45至65巴之壓力下 -29- 1.352614 操作，並產生做爲頂部產物之該預處理天然氣（111)， 此預處理天然氣（ill)實際上不再含有任何c6+烴類， 此輔助蒸餾塔還可產生基本上c6+重質烴類之餾份（105 ); 且該用於回收NGLS之單元（19 )包括： (cl)用於分離該冷卻之預處理天然氣（117)的分 離滾筒（47)，此滾筒產生液體股流（121)及氣體股流 (119)； (c2)用於使該氣體股流膨脹之第一膨脹渦輪機（51 )，該渦輪機係連結至第一壓縮機（53); (c3 )用於將該膨脹之氣體股流（129 )從該主塔（ 49 )的中間水平N3處導入該主塔（49 )的構件；以及 (c4 )用於使該液體股流（1 2 1 )膨脹之構件（1 23 ) 及用於將此膨脹之液體股流從該主塔（49 )之低於水平 N3之水平N2處導入該主塔（49 )的構件； 而且，該用於生成該可液化天然氣（161)之構件包 括用於將直接來自該預處理單元（17)之預處理天然氣（ 1 1 1 )的可調整部份（1 1 5 )選擇性地導入可液化天然氣管 線（1 6 1 )之構件。 1 1 ·如申請專利範圍第1 0項之設備，其中，該用於 生成該可液化天然氣（161)之構件（53、55、41)包括 (d 1 )用於在液化壓力下使從該主塔（49 )頂部提取 之純化天然氣（151)壓縮的構件（53、55)，其包括至 S -30- 1352614 少該第一壓縮機（53 );及 (d2)第一熱交換器（41)，其使來自該壓縮構件（ 53、55 )之經壓縮純化天然氣（155 )與從該主塔（49 ) 頂部所提取之該純化天然氣（151)產生熱交換關係，該 經壓縮純化天然氣（155)在此第一熱交換器（41)中冷 卻以便產生該可液化天然氣（161)。 12.如申請專利範圍第11項之設備，其中該用於冷 卻該預處理天然氣（111)之構件（43)包括使此氣體（ 1 1 1 )與從該主塔（49 )所提取之該純化天然氣（1 5 1 )產 生熱交換關係的第二熱交換器（43)。 1 3 .如申請專利範圍第n或1 2項之設備，其中該用 於壓縮從該主塔（49 )頂部所提取之純化天然氣（1 5 1 ) 的構件（5 3、5 5 )進一步包括藉由外來能源驅動且意欲用 來使該經壓縮之純化天然氣（1 5 5 )的壓力增高至該液化 壓力的第二壓縮機（55)。 -31 -
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